Integrated configuration for a steam assisted gravity drainage central processing facility

ABSTRACT

A steam assisted gravity drainage (SAGD) processing facility comprising: an oil/water separation process block operable for bulk separation of produced water from a produced fluid comprising produced water and hydrocarbons; a de-oiling process block operable to remove residual oil from the produced water separated from the produced fluid in the oil/water separation process block and provide a de-oiled water; a water treatment block operable to remove contaminants from the de-oiled water and provide a treated water; and a steam generation process block operable to produce steam from the treated water. In embodiments, each of the oil/water separation process block, the de-oiling process block, the water treatment process block, and the steam generation process block is modularized and comprises a plurality of modules. Methods for operating and assembling a SAGD processing facility are also provided.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a divisional of U.S. patent application Ser. No.16/165,240, filed Oct. 19, 2018 and entitled “Integrated Configurationfor a Steam Assisted Gravity Drainage Central Processing Facility”,which claims priority to U.S. Provisional Patent Application No.62/575,209, filed Oct. 20, 2017 and entitled “Integrated Configurationfor a Steam Assisted Gravity Drainage Central Processing Facility”, thedisclosures of which are both hereby incorporated herein by reference asif reproduced in its entirety.

STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR DEVELOPMENT

Not applicable.

REFERENCE TO A MICROFICHE APPENDIX

Not applicable.

TECHNICAL FIELD

The present disclosure relates to a steam assisted gravity drainage(SAGD) processing facility; more particularly, this disclosure relatesto a SAGD processing facility comprising mechanical vapor recompression(MVR) evaporation and conventional steam generation; still moreparticularly, this disclosure relates to a modularized SAGD processingfacility.

BACKGROUND

Steam Assisted Gravity Drainage (SAGD) is a thermal process forproduction of bitumen from oil sands reservoirs. The process involvesinjecting high pressure, saturated steam into the oil sands reservoir,which, upon contact with the colder oil sand, condenses to water, thusreleasing thermal energy. The released thermal energy heats andmobilizes the bitumen, so that it can be produced to the surface. Thethermal heating of the bitumen produces a small amount ofnon-condensable gas. At the surface, the stream of bitumen, thecondensed water, and produced gas are sent to a Central ProcessingFacility (CPF), also referred to herein as a ‘SAGD processing facility’,where the bitumen and water are separated, and the separated water istreated and heated to produce high pressure steam, which is sent back tothe reservoir.

SUMMARY

Herein disclosed is a steam assisted gravity drainage (SAGD) processingfacility comprising: an oil/water separation process block operable forbulk separation of produced water from a produced fluid comprisingproduced water and hydrocarbons, wherein the oil/water separationprocess block comprises an inlet for the produced fluid and an outletfor the produced water separated from the produced fluid; a de-oilingprocess block operable to remove residual oil from the produced waterseparated from the produced fluid in the oil/water separation processblock and provide a de-oiled water, wherein the de-oiling process blockcomprises an inlet for the produced water from the oil/water separationblock and an outlet for the de-oiled water; a water treatment blockoperable to remove contaminants from the de-oiled water and provide atreated water, wherein the water treatment process block comprises aninlet for the de-oiled water and an outlet for the treated water; and asteam generation process block operable to produce steam from thetreated water, wherein the steam generation process block comprises aninlet for the treated water and an outlet for steam, wherein: each ofthe oil/water separation process block, the de-oiling process block, thewater treatment process block, and the steam generation process block ismodularized and comprises a plurality of modules; the de-oiling processblock comprises a compact flotation unit, the water treatment processblock comprises a mechanical vapor recompression evaporation apparatus,the steam generation process block does not comprise a once throughsteam generator (OTSG), or a combination thereof; the SAGD processingfacility comprises no pressure reduction apparatus, no temperaturereduction apparatus, or both no pressure reduction apparatus and notemperature reduction apparatus to reduce the pressure or thetemperature, respectively, of the produced water separated from theproduced fluid in the oil/water separation process block prior tointroduction of the separated produced water into the de-oiling processblock; or a combination thereof.

Also disclosed herein is a method for operating a steam assisted gravitydrainage processing facility, the method comprising: effecting bulkseparation of produced water from a produced fluid comprising theproduced water and hydrocarbons; removing residual oil from the producedwater to provide a de-oiled water; removing contaminants from thede-oiled water to provide a treated water; and generating steam from thetreated water, wherein: each of the effecting bulk separation, theremoving residual oil, the removing contaminants, and the generatingsteam is performed via a plurality of modules; the removing residual oilfrom the produced water is effected via compact flotation, the removingcontaminants from the de-oiled water is effected via mechanical vaporrecompression evaporation, the generating steam from the treated wateris not effected via a once through steam generator (OTSG), or acombination thereof; the temperature, the pressure, or both thetemperature and the pressure of the produced water separated from theproduced fluid via the bulk separation is not reduced prior to removingresidual oil from the produced water; or a combination thereof.

Further disclosed herein is a method for assembling a steam assistedgravity drainage (SAGD) processing facility, the method comprising:providing a plurality of modules for each of a number of process blocksincluding: an oil/water separation process block (a) operable for bulkseparation of produced water from a produced fluid comprising theproduced water and hydrocarbons, wherein the oil/water separationprocess block comprises an inlet for the produced fluid and an outletfor the produced water separated from the produced fluid; a de-oilingprocess block (b) operable to remove residual oil from the producedwater separated from the produced fluid in the oil/water separationprocess block and provide a de-oiled water, wherein the de-oilingprocess block comprises an inlet for the produced water from theoil/water separation block and an outlet for de-oiled water; a watertreatment block (c) operable to remove contaminants from the de-oiledwater and provide a treated water, wherein the water treatment processblock comprises an inlet for the de-oiled water and an outlet for thetreated water; and a steam generation process block (d) operable toproduce steam from the treated water, wherein the steam generationprocess block comprises an inlet for the treated water and an outlet forsteam, wherein each process block (a), (b), (c), and (d) includes anelectrical and instrumentation (E&I) room on at least one of theplurality of modules for that process block; interconnecting theplurality of modules within process blocks (a), (b), (c), and (d);connecting process blocks (a) and (b), (b) and (c), and (c) and (d); andconnecting each E&I room with a central control room and a mainelectrical supply.

Also disclosed herein is a steam assisted gravity drainage (SAGD)processing facility comprising: an oil/water separation process blockoperable for bulk separation of produced water from a produced fluidcomprising the produced water and hydrocarbons, wherein the oil/waterseparation process block comprises an inlet for the produced fluid andan outlet for the produced water separated from the produced fluid; ade-oiling process block operable to remove residual oil from theproduced water removed from the oil/water separation process block andprovide a de-oiled water, wherein the de-oiling process block comprisesa compact flotation unit comprising an inlet for the produced water fromthe oil/water separation block and an outlet for the de-oiled water; awater treatment block operable to remove contaminants from the de-oiledwater and provide a treated water, wherein the water treatment processblock comprises mechanical vapor recompression evaporation apparatuscomprising an inlet for the de-oiled water and an outlet for the treatedwater; and a steam generation process block operable to produce steamfrom the treated water, wherein the steam generation process blockcomprises a boiler comprising an inlet for the treated water and anoutlet for steam, wherein each of the oil/water separation processblock, the de-oiling process block, the water treatment process block,and the steam generation process block is modularized and comprises aplurality of modules.

BRIEF DESCRIPTION OF THE DRAWINGS

For a more complete understanding of the present disclosure and theadvantages thereof, reference is now made to the following briefdescription, taken in connection with the accompanying drawings anddetailed description, wherein like reference numerals represent likeparts.

FIG. 1 is a schematic of a typical steam assisted gravity drainage(SAGD) processing facility I;

FIG. 2 is a schematic of a SAGD processing facility II, according to anembodiment of this disclosure;

FIG. 3 shows an exemplary equipment module 200, according to anembodiment of this disclosure;

FIG. 4 shows the exemplary equipment module 200 of FIG. 4 interconnectedwith a piping module 200A directly thereabove, according to anembodiment of this disclosure; and

FIG. 5 is an exemplary plot plan of a SAGD processing facility III,according to an embodiment of this disclosure.

DETAILED DESCRIPTION

It should be understood at the outset that although illustrativeimplementations of one or more embodiments are illustrated below, thedisclosed systems and methods may be implemented using any number oftechniques, whether currently known or not yet in existence. Thedisclosure should in no way be limited to the illustrativeimplementations, drawings, and techniques illustrated below, but may bemodified within the scope of the appended claims along with their fullscope of equivalents.

The following brief definition of terms shall apply throughout theapplication:

The term “comprising” means including but not limited to, and should beinterpreted in the manner it is typically used in the patent context;

The phrases “in one embodiment,” “according to one embodiment,” “in someembodiments,” and the like generally mean that the particular feature,structure, or characteristic following the phrase may be included in atleast one embodiment of the present invention, and may be included inmore than one embodiment of the present invention (importantly, suchphrases do not necessarily refer to the same embodiment);

If the specification describes something as “exemplary” or an “example,”it should be understood that refers to a non-exclusive example;

The terms “about” or “approximately” or the like, when used with anumber, may mean that specific number, or alternatively, a range inproximity to the specific number, as understood by persons of skill inthe art field; and

If the specification states a component or feature “may,” “can,”“could,” “should,” “would,” “preferably,” “possibly,” “typically,”“optionally,” “for example,” “often,” or “might” (or other suchlanguage) be included or have a characteristic, that particularcomponent or feature is not required to be included or to have thecharacteristic. Such component or feature may be optionally included insome embodiments, or it may be excluded.

SAGD processing will now be described briefly to facilitate descriptionof the herein-disclosed SAGD processing herein below. A typical SAGDprocess is shown in FIG. 1, which is a schematic of a typical steamassisted gravity drainage (SAGD) processing facility I. At the CPF,there may be a number of main processing steps or blocks. For example,the SAGD processing may comprise an oil/water separation step or block10, a de-oiling step or block 30, a water treatment step or block 40,and a steam generation step or block 50. The CPF may further comprise aproduced gas collection step or block 20, a disposal water treatmentstep or block 60, a hydrocarbon storage step or block 70, a vaporrecovery step or block 80, a slops and de-sanding step or block 90, aglycol heating and cooling step or block 100, and/or a utilities step orblock 110. These processing steps or blocks will be described in moredetail herein below, and may be referred to simply as blocks. The blockscan comprise one or more apparatus for carrying out the step.

At oil/water separation block 10, bulk separation of produced water fromproduced well pad 5 (which can be an emulsion comprising oil, water,gas, and/or entrained solids) is effected. For example, in someembodiments, a light hydrocarbon diluent, such as naphtha or condensate,may be added to the produced fluid stream line 6, comprising oil (e.g.,bitumen) and water, from well pads 5 to reduce the density and viscosityof the oil phase such that it floats on water and therefore can beseparated via traditional gravity separation techniques. Oil/waterseparation 10 can comprise a first oil/water separation 10A and a secondoil/water separation 10B. First oil/water separation 10A can comprisefree water knockout (FWKO) and second oil/water separation 10B cancomprise an oil/water treater, such as a gravity separator. In someembodiments, diluent is routed via diluent line 71 from hydrocarbonstorage 70, which is described further herein below. Separated oil maybe introduced into hydrocarbon storage 70 via produced oil line 12.Produced water may be removed from oil/water separation 10 via producedwater line 11. Produced gas removed from the emulsion in oil/waterseparation 10 can be introduced into produced gas collection step orblock 20 via produced gas line 13. As indicated in the embodiment ofFIG. 1, chemicals (CH), such as demulsifiers, surfactants, and the likecan be utilized in oil/water separation 10, and slop liquids (SL),including de-sand fluid and a rag layer, may be removed from oil/waterseparation 10, and introduced into slops and de-sanding block 90, whichis described further herein below.

The SAGD processing may comprise a de-oiling step or block 30, in whichthe produced water from the oil/water separation step or block 10 inproduced water line 11 may be processed to remove residual oil down tominimum levels required by the downstream processing steps, thusproviding a de-oiled water in line 31. As depicted in the embodiment ofFIG. 1, chemicals (CH), such as demulsifiers, surfactants, flocculants,and the like, may also be introduced into de-oiling 30. As depicted inthe embodiment of FIG. 1, de-oiling 30 is traditionally performed in athree step process, each step of which (e.g., gravity separation 30A,flotation 30B, and media filtration 30C) is conventionally operated atatmospheric conditions, requiring the produced water to be cooled tobelow 100° C. The first step 30A is typically gravity separation, thesecond step 30B typically includes gas flotation, in which gas may beinjected into the water to enhance oil separation, and the third step30C typically includes conventional media filtration. In someembodiments, condensed liquids from a produced gas separator in producedgas collection step or block 20 (described further herein below) mayalso be introduced into de-oiling step or block 30 via condensed liquidsline 21. De-oiled water may be removed from de-oiling block 30 viade-oiled water line 31. In some embodiments, de-oiled water may bestored in a de-oiled water storage step, apparatus, or block 35, andmake-up water introduced thereto, as necessary, via make-up water line32.

As noted above, the SAGD processing may comprise a water treatment stepor block 40, in which the de-oiled water obtained from de-oiling step orblock 30 (via de-oiled water line 31) or from de-oiled water storagestep or block 35 (via stored de-oiled water line 33) may be furthertreated to remove contaminants down to minimum levels required by thedownstream steam generation process. Typically, the water treatment is atwo stage process, including a softening step 40A in which chemicals(CH), such as lime and magnesium oxide, may be used for silica removal,and a conventional ion exchanger step 40B to remove hardness. Steamgeneration blowdown from steam generation step or block 50 (describedfurther herein below) may be introduced into water treatment 40 viasteam generation blowdown line 51. Treated water may be removed fromwater treatment step or block 40 via treated water line 42. Lime sludgesolids may be removed from water treatment step or block 40 via limesludge line 41 and sent for disposal via solids disposal line 63A. Insome embodiments, treated water may be stored in a boiler feed water(BFW) storage step, apparatus, or block 45.

As noted hereinabove, the SAGD processing may comprise a steamgeneration step or block 50, in which the treated water (from watertreatment step or block 40 via treated water line 42 or from BFW storage45 via stored, treated water line 46) may be used as boiler feed water(BFW) to produce high pressure, saturated injection steam. As depictedin the embodiment of FIG. 1, chemicals (CH), such as, withoutlimitation, dispersant, phosphate, neutralizing amine, filming amine,oxygen scavenger, and fuel gas (FG), may also be introduced into andutilized by steam generation 50. The type of steam generator useddepends on the BFW quality.

Conventionally, BFW from the softening/ion-exchange process 40A/40B (ofthe water treatment step or block 40) may not meet industry norms foruse of conventional steam generators. Therefore, once through steamgenerators (OTSGs) may be required. OTSGs only produce nominally 75-80%steam quality at the discharge (within block 50, e.g., in high pressuresteam outlet line 52), requiring that the residual hot water stream atthe steam generation discharge (e.g., about 20-25% of the total BFWflow) be recycled within the overall process. For example, in theembodiment of FIG. 1, a portion of the steam generator blowdown isrecycled via steam generator blowdown line 51 to water treatment 40 andanother portion of the steam generator blowdown is sent to disposalwater treatment step or block 60 (also referred to as disposal waterReduced Liquid Discharge (RLD) treatment step or block 60) via steamgenerator blowdown line 53. In embodiments, the disposal water treatmentstep or block 60 concentrates blowdown using steam or mechanical vaporrecompression to evaporate a portion of the influent water. As depictedin FIG. 1, the high pressure steam in high pressure steam line 52 fromsteam generation 50 is reintroduced into well pads 5 for further bitumenextraction via SAGD.

The SAGD processing may further comprise a disposal water treatment stepor block 60, in which the blowdown from the steam generation step orblock 50 may be processed to recover water to meet regulatoryrequirements for water usage. Chemicals (CH), such as caustic, sulfuricacid, hydrochloric acid, and chelant, may also be introduced intodisposal water treatment 60, as depicted in the embodiment of FIG. 1.When OTSGs are utilized for the steam generation step 50, the steamgenerator blowdown may be sent to the disposal water treatment unit ofdisposal water treatment step or block 60 (e.g., via steam generatorblowdown line 53), where it may be concentrated (e.g., via an MVRprocess), producing a solids stream in solids disposal line 63 and/or aconcentrated water stream in concentrated disposal brine line 62, whichmay be sent offsite for disposal. For example, lime sludge solids inlime sludge solids line 41 from water treatment 40 and disposal solidsin solids disposal line 63 may be combined and sent for disposal viasolids disposal line 63A. Recovered water may be recycled via recoveredwater line 61, for example, to BFW storage 45. As mentioned hereinabove,the SAGD processing may further comprise hydrocarbon storage step,apparatus, or block 70, wherein diluent from a pipeline in pipelinediluent line 71A and separated hydrocarbons in separated hydrocarbonline 12 from oil/water separation 10 can be stored. Recoveredhydrocarbons can be sent offsite via line 12A from hydrocarbon storage70, for example, to a pipeline for sale. A portion of the diluent inhydrocarbon storage 70 can be introduced into oil/water separation 10via diluent line 71, and hydrocarbons separated from produced water andgas in oil/water separation 10 can be introduced into hydrocarbonstorage 70 via separated hydrocarbon line 12. Offgas from hydrocarbonstorage 70 can be recovered, via offgas line 72, by vapor recovery step,apparatus, or block 80.

As mentioned hereinabove, the SAGD processing may further comprise vaporrecovery step, apparatus, or block 80, wherein offgas from hydrocarbonstorage 70 is processed into hydrocarbon vapor in hydrocarbon vapor line81, flare gas in flare gas line 82, and/or recovered liquids inrecovered liquids line 83. The hydrocarbon vapor in hydrocarbon vaporline 81 can, in some embodiments, be introduced into produced gascollection step, apparatus, or block 20. The flare gas in flare gas line82 is sent to flare for disposal. The recovered liquids in recoveredliquids line 83 can, in some embodiments, be sent to slops andde-sanding step, apparatus, or block 90.

As mentioned hereinabove, the SAGD processing facility may furthercomprise produced gas collection or handling step, apparatus, or block20, wherein a gas separator may be utilized to separate condensedliquids from the gas introduced into produced gas collection 20.Hydrocarbon vapor in hydrocarbon vapor line 81, natural gas (NG) from apipeline, and/or produced gas in produced gas line 13 can be introducedinto produced gas collection 20. Chemicals (CH), such as corrosioninhibitor and methanol, may also be introduced into produced gascollection 20. As noted hereinabove, the condensed liquids may beintroduced into de-oiling 30 via condensed liquids line 21. Theremaining gas may be extracted as fuel gas (FG) from produced gascollection 20. The fuel gas may be utilized for glycol heating andcooling in glycol heating and cooling step, apparatus, or block 100and/or for steam generation in steam generation 50, as indicated in theembodiment of FIG. 1.

A SAGD processing facility can further comprise slops and de-sandingstep, apparatus, or block 90 configured to subject slop liquids tocollection and processing for oil/water separation or removal from theSAGD processing facility (e.g., to segregate sand and recalcitrantemulsion for offsite disposal), a glycol heating and cooling step,apparatus, or block 100 configured to facilitate heat recovery andrejection throughout the facility and utilize fuel gas (e.g., naturalgas and/or gas from produced gas collection 20) as a heat input to theprocess (e.g., to heat glycol for use as a process heating medium),and/or utilities step, apparatus, or block 110 configured to provideinstrument air and natural gas distribution for the SAGD facility.

Typical SAGD developments may be built implementing the technologiesdescribed above, for example using conventional design and executionstrategies for fabrication and construction of the facilities. Theseapproaches may not sufficiently leverage best-in-class technologies, nordo they sufficiently implement leading technologies for fabrication andconstruction, such as advanced modularization. As such, future SAGDdevelopments utilizing conventional designs may not meet desiredeconomic targets, e.g. net present value or rate of return.

Embodiments disclosed herein may comprise a process comprising amodified design and execution of SAGD CPF facilities through optimalimplementation of best-in-class technologies, building on availablesynergies to arrive at a functional design with minimum scope, andoptimal packaging of the required scope (e.g., through application ofadvance modularization approaches, in some embodiments), resulting in abest-in-class capital cost design. Such design may provide aneconomically viable solution for the CPF component of SAGD projects overthe project life (e.g., in a long term low oil price environment). Anembodiment of a process may comprise selection and integration ofbest-in-class technologies into an optimal process configuration.Additionally, an embodiment may comprise packaging of the optimizedproject scope (mechanical, electrical and instrumentation equipment andbulk materials) in an advanced modular design.

The process flow configuration for a proposed embodiment is shown inFIG. 2, which is a schematic of a SAGD processing facility II, accordingto an embodiment of this disclosure. In the embodiment shown in FIG. 2,an optimal process configuration may be achieved via implementation ofone or more improved technologies. Unless otherwise noted, the processsteps, apparatus, or blocks of FIG. 2 may be as described with regard tothe embodiment of FIG. 1, and will not be reiterated here.

In some embodiments, oil/water separation 10 comprises primary oil/waterseparation via a FWKO and secondary oil/water separation via an optionaldiluent based degassing via diluent based oil treating (e.g., additionof hydrocarbon from hydrocarbon storage 70 via diluent line 71). In someembodiments, oil/water separation 10 comprises optional degassing via apressure reduction vessel and emulsion degassing vessel. The optionaldegassing may change the operating conditions (e.g., the pressureprofile) relative to typical SAGD CPFs. For example, a conventional SAGDCPF will limit the pressure drop of the emulsion from the battery limitto avoid installing pumps between oil/water separation 10 andhydrocarbon storage 70. Light hydrocarbon may be added to effect theoil/water separation step 10, for example, via diluent line 71 fromhydrocarbon storage 70. In some embodiments, the produced water inproduced water line 11 from oil/water separation 10 has a temperature ina range of from about 125° C. to about 140° C. In some embodiments, theproduced water in produced water line 11 from oil/water separation 10has a pressure in a range of from about 800 kPa to about 1200 kPa.

In some embodiments, compact flotation (e.g., via at least one compactflotation unit (CFU)) is utilized for the de-oiling at 30. CFUtechnology combines centrifugal separation and gas flotation into asingle pressure vessel, which can be operated at elevated pressures andtemperatures. Accordingly, in some embodiments, the produced waterseparated from the produced fluid at oil/water separation 10 is notsubjected to temperature and/or pressure reduction prior to introductioninto de-oiling 30. In some embodiments, the produced water in producedwater line 11 is not stored prior to introduction into de-oiling 30.Compact flotation technology, rather than conventional technology, suchas gas flotation, enables de-oiling 30 to be pressurized, and eliminatesthe need for cooling and then reheating the water, by allowing the waterto remain hot throughout the de-oiling 30 and water treatment 40.

In some embodiments, the de-oiled water in de-oiled water line 31 fromde-oiling 30 has a temperature in a range of from about 115° C. to about140° C. In some embodiments, the de-oiled water in de-oiled water line31 from de-oiling 30 has a pressure in a range of from about 800 kPag toabout 1200 kPag.

In some embodiments, the de-oiled water is stored in a de-oiled waterstorage apparatus 35. In some embodiments, the de-oiled water storageapparatus comprises a pressure vessel (e.g., is not an atmosphericstorage vessel), and thus requires no additional containment.

In some embodiments, water treatment step, apparatus, or block 40utilizes mechanical vapor recompression (MVR) evaporation technology,rather than conventional water treatment (e.g., comprising limesoftening 40A and ion exchange 40B, as described with reference to theembodiment of FIG. 1). MVR evaporation comprises a simple distillationprocess that can be employed to produce a distillate water streamsuitable for use in conventional steam generation systems (e.g.,non-OTSGs). MVR is an energy recovery process wherein compression isutilized to add energy to lower pressure water vapor to produce amarginally smaller volume of vapor at a higher temperature and pressure;the compressed vapor is then utilized to heat the de-oiled water toproduce additional low pressure vapor. In some embodiments, the treatedwater in treated water line 42 (and/or the stored, treated water instored treater water line 46) has a temperature in a range of from about115° C. to about 130° C. In some embodiments, the treated water intreated water line 42 from water treating 40 (and/or stored treaterwater in stored, treated water line 46 from BFW storage 45) has apressure in a range of from about 400 kPag to about 800 kPag. In someembodiments, the treated water in treated water line 42 (and/or thestored, treated water in stored, treater water line 46) can compriseminor amounts of contaminants, such as hydrocarbons, salts, and thelike.

When utilizing MVR at water treatment 40, lime sludge can besubstantially or completely avoided, and in some embodiments, may not beneeded. In such embodiments, a line 41A may be utilized to removecontaminants from the MVR evaporation of water treatment 40. When MVRand conventional steam generators are used, the concentrate stream 41Afrom the MVR unit may be sent to the disposal water treatment system 60,again producing a solids stream 63 and/or a concentrated brine stream 62which may be sent offsite for disposal.

In some embodiments, the treated water in treated water line 42 isstored in a BFW storage apparatus 45. In some embodiments, the BFWstorage apparatus 45 comprises a pressure vessel (e.g., is not anatmospheric storage vessel), and thus requires no additionalcontainment.

In some embodiments, the treated water (e.g., the BFW) in line 42/46 isa high quality water that is sufficiently uncontaminated thatconventional steam generators (e.g., drum boilers and/or circulationboilers, rather than OTSGs) can be utilized, optionally with somemodifications, at steam generation 50. In some embodiments, BFW from theMVR process is of such higher quality that conventional steamgenerators, optionally with some modifications, can be used to producesteam quality in the range of at least 94, 95, 96, or 97% or higher.Such conventional steam generators may be more easily modularized thanOTSGs, and enable a further reduction in the footprint of a SAGDprocessing facility of this disclosure. Such modularized steamgenerators can require less on-site field fabrication than OTSGs.

The use of MVR technology in water treatment 40 may also (via providingwater of a quality sufficient for the use of conventional steamgenerators in steam generation 50) enable elimination of the hot waterrecycle in steam generator blowdown line 53, and thus such a line 53 maynot be employed in a SAGD processing facility, such as SAGD processingfacility II, according to embodiments of this disclosure. Similarly,steam generation blowdown in steam generation blowdown line 51 may bereduced (e.g., to 2% to 5%) as opposed to a steam generation blowdown ina steam generation blowdown line 51 produced via a steam generation 50comprising OTSG(s). Elimination or reduction of blowdown from the steamgeneration 50 can, in some embodiments, reduce the footprint and scopetraditionally needed for separating such blowdown water from steam andrecovering additional portions of that blowdown water (e.g., via flashor a dedicated evaporative system). Steam generation may utilizecogeneration technology, whereby electricity and steam are produced.

As noted hereinabove, a SAGD CPF of this disclosure can further comprisea disposal water treatment 60. A disposal water treatment step,apparatus, or block 60 may, in some embodiments, utilize modifiedtechnology, possibly as a result of implementing the MVR process forwater treatment 40. In some embodiments, disposal water treatment 60effects primarily or solely solids separation. Such solids separationmay comprise, for example, filtration. In some embodiments, the use ofMVR evaporation at water treatment 40 may result in a concentrated brinefor disposal in concentrated brine disposal line 62. In someembodiments, the use of MVR evaporation at water treatment 40 may resultin a recovered water in recovered water line 61.

In some embodiments, optimized packaging of the scope may be achievedvia the use of Fluor's patented 3^(rd) Gen Modular Execution℠ designmethodology, which is described in U.S. Pat. No. 8,931,217 and U.S.patent application Ser. No. 15/440,812, the disclosure of each of whichis hereby incorporated herein by reference except to the extent it mightdirectly conflict with the present disclosure.

Key concepts of the 3rd Gen design process will now be describedbriefly. The overall process may be broken down into individual processblocks, such as noted hereinabove with reference to a SAGD facility ofthis disclosure. The detailed design of each process block may be thenphysically arranged within one or more modules to optimize the synergybetween the equipment and the associated piping, electrical, and controlsystems. These modules may be then laid out synergistically, based onthe overall process flow between the process blocks, to minimize thenumber and lengths of the required module interconnects. In someembodiments, process blocks and/or modules forming process blocks arenot connected via external piping (e.g., via pipe racks), but areinterconnected directly (e.g., with such connection typically locatedwithin the envelopes of the relevant process blocks). Techniques may beused to maximize the amount of equipment, including rotating equipment,which may be installed in modules. Modules may be designed based onweight and weight distribution (e.g., center of gravity) limits, moduleflexing/distortion, vibration limits (on operation and/or transport),size limits, maintainability (in view of space limitations driven byhigh density modularization), interconnections of modules and connectionof modules to (e.g., underground) fiber optic backbone and/or mainelectrical supply at the site, integration of E&I systems intoindividual modules with E&I systems unfriendly environments, locationand heat management of major power equipment within modules, and thelike, such that the modules can be safely transported (e.g., via railand/or truck) and positioned on-site. By way of example, heat exchangerselection (e.g., shell and tube, plate and frame, or plate and shell)may be made and the size/arrangement thereof selected to suit themodularization approach.

The modules may be broken down into two primary types: equipment modulesand pipeway modules. Equipment modules may contain primarily equipment,but also some piping, which connects equipment within the same module,and electrical cable. Pipeway modules can contain primarily piping,which interconnects equipment and systems between modules or processblocks. In some embodiments, the pipeway modules may be situateddirectly above the equipment modules, thus minimizing theinterconnecting piping lengths. In some embodiments, drain systems maybe integrated into the module(s), below the floor level, to eliminatethe need for underground piping. In some embodiments, a distributedelectrical and instrumentation (E&I) system may be implemented, wherethe design is configured so that electrical rooms and control systemscabinets can be installed on modules, maximizing the amount ofelectrical equipment and instrumentation to be installed, wired, andtested on the modules, rather than on-site. In some embodiments, eachprocess block (e.g., oil/water separation process block 10, produced gascollection process block 20, de-oiling process block 30, water treatmentprocess block 40, steam generation process block 50, disposal watertreatment block 60, hydrocarbon storage process block 70, vapor recoveryprocess block 80, slops and de-sanding process block 90, glycol heatingand cooling process block 100, and/or utilities process block 110)comprises at least one distributed E&I room on at least one module ofthe process block, and each such distributed E&I room is incommunication (e.g., via fiber optic cable which may or may not beunderground) with a central control room. For example, a SAGD processingfacility of this disclosure may comprise 5, 6, 7, 8, 9, or 10distributed E&I rooms connected to a central control room. Suchdistributed E&I can, in some embodiments, reduce the on-site field workrequired to prepare the modularized SAGD processing facility of thisdisclosure for operation. Similarly, in some embodiments, electricaldistribution from the main electrical supply to the individualelectrical rooms may be done underground (e.g., with each process blocktypically having its own electrical room for electrical and instruments(E & I) for that process block).

The modules are designed to easily interconnect in a predetermined wayonce transported to the on-site location for the SAGD processingfacility. The modules may be designed as ‘plug-and-play’ modules,wherein modules are self-contained, high-density, pre-tested modulesrequiring primarily or substantially solely interconnections at thesite. By way of example, FIG. 3 shows an exemplary equipment module 200,according to an embodiment of this disclosure. Equipment module 200comprises E&I room 210 and a variety of equipment 220. E&I room 210 isin communication with equipment 220, and also with a main electricalsupply (not shown in FIG. 3) and a central control room (also not shownin FIG. 3). FIG. 4 shows the exemplary equipment module 200 of FIG. 4interconnected with a piping module 200A directly thereabove, to provideintegrated/interconnected binary module 250 according to an embodimentof this disclosure.

In some embodiments, the various processes of FIG. 2 may be carried outby a plurality of process blocks (e.g., with at least one process blockfor each such process of FIG. 2), which may be designed, configured,and/or connected as discussed herein (e.g., using modularizationtechnologies and/or a ‘zero base’ engineering approach whereintraditionally used design margins are eliminated, resulting in minimizedredundancy and equipment overcapacity). To assist in module connection,each such process block may comprise one or more (e.g., a plurality of)modules. Thus, as per this disclosure, modularization technologies maybe applied to a SAGD processing facility. In some embodiments, amodularized SAGD processing facility according to this disclosure canprocess produced fluid at a rate of at least 30, 35, or 40 KBPD (i.e.,30, 35, or 40 thousand barrels per day of bitumen) or in a range of from30 to 110, from 40 to 110, or from 50 to 100 KBPD, and comprises lessthan about 50, 60, or 70 total (e.g., equipment plus piping) modules, orfrom about 30 to 100, from 40 to 90, or from 40 to 60 total modules. Insome embodiments, a modularized SAGD processing facility according tothis disclosure can process produced fluid at a rate of at least 20, 35,or 30 KBPD, or from 20 to 25, 10 to 25, or 10 to 20 KBPD, and comprisesless than about 40, 50 or 60 equipment modules, or from about 40 to 60,from 40 to 70, or from 50 to 60 modules.

Accordingly, in some embodiments, the number of modules and overallsystem cost of a SAGD processing facility may be reduced by pursuingadvancements in modularization technology leading to higherplug-and-play functionality, and higher module equipment density asdescribed herein. Without limitation, such advancements may include oneor more of: (1) integration of pipeways with mechanical/E&I (electricaland instrumentation) modules; (2) employing distributed E&I (e.g.,moving E&I completion to module assembly yard); (3)imbedding/integrating traditionally underground process piping intomodule frames; (4) letting modularization constraints drive equipmentimplementation; (5) having the layout driven by modularization, ratherthan vice versa; (6) installing and testing a majority of the piping andE&I at the module assembly yard; (7) locating E&I equipment withinmodules and/or closer to the user; (8) employing underground fiber opticand/or power (e.g., electrical) distribution; and (9) installing amajority of the instrumentation and control within modules.

Some of the benefits of the process depicted in FIG. 2 and describedherein will now be described. Via the herein disclosed SAGD processingfacility and method, thermal energy in the production fluid from thefield may be retained within the process to the maximum extent possible.This may maximize overall energy efficiency and may minimize the amountof heat transfer equipment within the system. Pressure energy in theproduction fluid from the field may be retained within the process tothe maximum extent possible. This may minimize the energy required toproduce injection steam at the required battery limit conditions. Forexample, utilization of compact flotation (and a CFU) for de-oiling 30eliminates the need for pressure and/or temperature reduction of theproduced water upstream of and/or within de-oiling 30 and/or watertreatment 40, in some embodiments.

Process water recycled within the CPF may be minimized, minimizingand/or eliminating the need for equipment and systems to recycle waterwithin the CPF process. For example, the utilization of MVR evaporationat water treatment 40 and conventional (e.g., non-OTSG) steam generatorsat steam generation 50 may reduce or eliminate the blowdown recycled viasteam generation blowdown line 53 and or steam generation blowdown line51. In some embodiments, overall, total water consumption may beminimized.

There may be a reduction in the amount of solid waste from the processbeing sent to the landfill. The process configuration may reduce thetotal amount of equipment, resulting in a reduction in bulk materialquantities associated with that equipment, primarily in piping andelectrical materials. The reduced scope and implemented technologies ofthe SAGD processing facility of this disclosure may enhance the abilityto modularize equipment and systems off-site.

Additionally, the required scope to integrate the process systems(specifically piping and electrical materials) can be significantlyreduced beyond what would be possible if the proposed processconfiguration were packaged using conventional modularizationtechniques. More of the construction can be done in a controlledenvironment in a modular fabrication facility (e.g., away from the finalconstruction site for the facility as a whole), where work may be donemore safely, productively, predictably, and to a higher level ofquality, as compared to installation at the construction site, resultingin a lower total project cost. Pre-assembling the modules off-site tothe extent possible can reduce on-site construction costs and thusdecrease the overall construction cost (e.g., the total installationcost, TIC) of the facility. In some embodiments, the TIC is reduced atleast 10, 20, or 30% relative to a conventional SAGD processing facilityor a conventionally modularized SAGD processing facility.

As noted above, the piping and electrical interfaces between modules maybe minimized, in some embodiments, so there may be less field workrequired to execute connections in the field (e.g., at the SAGDprocessing facility). The process may provide the ability to performparallel construction at the site and at the module yard, potentiallyproviding opportunities to reduce the overall schedule. For example, theutilization of distributed E&I and/or an E&I room positioned on a moduleassociated with each main process step may enable a reduction in thenumber of connections between modules and/or process blocks, and/or forfewer connections between modules and a main electrical supply and/orfiber optic line. Design of the modularized SAGD processing facility asdescribed herein may allow electrical and/or fiber optic lines to be rununderground on-site (e.g., at the SAGD processing facility) in advanceof the modules being positioned at the site (e.g., concomitantly withmodule fabrication off-site).

The improved configuration may reduce the overall plot arearequirements, resulting in less land disturbance. In some embodiments,the herein-disclosed SAGD processing facility utilizes a highlymodularized approach to achieve a reduction in footprint, and/orinvestment of at least 15, 20, 25, or 30% without negatively impactingreliability, maintainability, and operating costs. In some embodiments,the herein-disclosed SAGD processing facility utilizes a highlymodularized approach to achieve a reduction in the number of modules(e.g., total number of modules and/or equipment modules), by at least30, 35, or 40%. In some embodiments, the herein-disclosed SAGDprocessing facility utilizes a highly modularized approach to achieve areduction in on-site installation man-hours and/or a combined labor andequipment/material cost of at least 35, 40, 45, or 50%. Energy use bythe SAGD processing facility may be reduced via the herein-disclosedSAGD processing facility. The herein-disclosed SAGD processing facilitycan be standardized, is easily replicable, is scalable, and may includecogeneration, as described hereinabove. The SAGD processing facility ofthis disclosure may be designed to provide a sufficiently wideprocessing window to accommodate at least 70, 75, or 80% of theprocessing conditions expected for a specific on-site location (e.g.,Alberta oil sands).

In some embodiments, a SAGD processing facility of this disclosure isutilized with enhanced-solvent SAGD (ES-SAGD), in which a hydrocarbonliquid is co-injected as a solvent with the steam. ES-SAGD may beutilized to reduce the volumetric steam to oil ratio (SOR). The solvent(minus some losses) is produced back to the well pads with the oil(e.g., bitumen). Persons of skill will appreciate these and otherpossible benefits and advantages to the present disclosure.

EXAMPLES

The embodiments having been generally described, the following examplesare given as particular embodiments of the disclosure and to demonstratethe practice and advantages thereof. It is understood that the examplesare given by way of illustration and are not intended to limit thespecification or the claims in any manner.

Example 1: Plot Plan of an Exemplary SAGD Processing Facility Accordingto this Disclosure

FIG. 5 is an exemplary plot plan of a SAGD processing facility III,according to an embodiment of this disclosure. Although other layoutsare envisioned and within the scope of this disclosure, FIG. 5illustrates how technology selection and modularization of the processblocks of a SAGD processing facility according to this disclosureprovides a reduced scope relative to conventional SAGD processingfacilities. SAGD processing facility III of the embodiment of FIG. 5comprises oil/water separation process block 10, produced gas collectionprocess block 20, de-oiling process block 30, de-oiled water storageprocess block 35, water treatment process block 40, BFW storage processblock 45, steam generation process block 50, disposal water treatmentprocess block 60, hydrocarbon storage process block 70, vapor recoveryprocess block 80, slop and de-sanding process block 90, glycol heatingand cooling process block 100, and utilities process block 110.

While various embodiments have been shown and described, modificationsthereof can be made by one skilled in the art without departing from thespirit and teachings of the disclosure. The embodiments described hereinare exemplary only, and are not intended to be limiting. Many variationsand modifications of the subject matter disclosed herein are possibleand are within the scope of the disclosure. Where numerical ranges orlimitations are expressly stated, such express ranges or limitationsshould be understood to include iterative ranges or limitations of likemagnitude falling within the expressly stated ranges or limitations(e.g., from about 1 to about 10 includes, 2, 3, 4, etc.; greater than0.10 includes 0.11, 0.12, 0.13, etc.). For example, whenever a numericalrange with a lower limit, R_(L) and an upper limit, R_(U) is disclosed,any number falling within the range is specifically disclosed. Inparticular, the following numbers within the range are specificallydisclosed: R=R_(L)+k*(R_(U)−R_(L)), wherein k is a variable ranging from1 percent to 100 percent with a 1 percent increment, i.e., k is 1percent, 2 percent, 3 percent, 4 percent, 5 percent, . . . 50 percent,51 percent, 52 percent, . . . , 95 percent, 96 percent, 97 percent, 98percent, 99 percent, or 100 percent. Moreover, any numerical rangedefined by two R numbers as defined in the above is also specificallydisclosed. Use of the term “optionally” with respect to any element of aclaim is intended to mean that the subject element is required, oralternatively, is not required. Both alternatives are intended to bewithin the scope of the claim. Use of broader terms such as comprises,includes, having, etc. should be understood to provide support fornarrower terms such as consisting of, consisting essentially of,comprised substantially of, etc.

Accordingly, the scope of protection is not limited by the descriptionset out above but is only limited by the claims which follow, that scopeincluding all equivalents of the subject matter of the claims. Each andevery claim is incorporated into the specification as an embodiment ofthe present disclosure. Thus, the claims are a further description andare an addition to the embodiments of the present disclosure. Thediscussion of a reference is not an admission that it is prior art tothe present disclosure, especially any reference that may have apublication date after the priority date of this application. Thedisclosures of all patents, patent applications, and publications citedherein are hereby incorporated by reference, to the extent that theyprovide exemplary, procedural, or other details supplementary to thoseset forth herein.

Additional Description

The particular embodiments disclosed above are illustrative only, as thepresent disclosure may be modified and practiced in different butequivalent manners apparent to those skilled in the art having thebenefit of the teachings herein. Furthermore, no limitations areintended to the details of construction or design herein shown, otherthan as described in the claims below. It is therefore evident that theparticular illustrative embodiments disclosed above may be altered ormodified and all such variations are considered within the scope andspirit of the present disclosure. Alternative embodiments that resultfrom combining, integrating, and/or omitting features of theembodiment(s) are also within the scope of the disclosure. Whilecompositions and methods are described in broader terms of “having”,“comprising,” “containing,” or “including” various components or steps,the compositions and methods can also “consist essentially of” or“consist of” the various components and steps. Use of the terms“optionally,” “may,” “might,” “possibly,” and the like with respect toany element of a claim means that the element is required, oralternatively, the element is not required, both alternatives beingwithin the scope of the embodiments. Also, references to examples aremerely provided for illustrative purposes, and are not intended to beexclusive.

Numbers and ranges disclosed above may vary by some amount. Whenever anumerical range with a lower limit and an upper limit is disclosed, anynumber and any included range falling within the range are specificallydisclosed. In particular, every range of values (of the form, “fromabout a to about b,” or, equivalently, “from approximately a to b,” or,equivalently, “from approximately a-b”) disclosed herein is to beunderstood to set forth every number and range encompassed within thebroader range of values. Also, the terms in the claims have their plain,ordinary meaning unless otherwise explicitly and clearly defined by thepatentee. Moreover, the indefinite articles “a” or “an”, as used in theclaims, are defined herein to mean one or more than one of the elementthat it introduces. If there is any conflict in the usages of a word orterm in this specification and one or more patent or other documents,the definitions that are consistent with this specification should beadopted.

Additionally, the section headings used herein are provided forconsistency with the suggestions under 37 C.F.R. 1.77 or to otherwiseprovide organizational cues. These headings shall not limit orcharacterize the invention(s) set out in any claims that may issue fromthis disclosure. Specifically and by way of example, although theheadings might refer to a “Field,” the claims should not be limited bythe language chosen under this heading to describe the so-called field.Further, a description of a technology in the “Background” is not to beconstrued as an admission that certain technology is prior art to anyinvention(s) in this disclosure. Neither is the “Summary” to beconsidered as a limiting characterization of the invention(s) set forthin issued claims. Furthermore, any reference in this disclosure to“invention” in the singular should not be used to argue that there isonly a single point of novelty in this disclosure. Multiple inventionsmay be set forth according to the limitations of the multiple claimsissuing from this disclosure, and such claims accordingly define theinvention(s), and their equivalents, that are protected thereby. In allinstances, the scope of the claims shall be considered on their ownmerits in light of this disclosure, but should not be constrained by theheadings set forth herein.

Embodiments disclosed herein include:

A: A steam assisted gravity drainage (SAGD) processing facilitycomprising: an oil/water separation process block operable for bulkseparation of produced water from a produced fluid comprising producedwater and hydrocarbons, wherein the oil/water separation process blockcomprises an inlet for the produced fluid and an outlet for the producedwater separated from the produced fluid; a de-oiling process blockoperable to remove residual oil from the produced water separated fromthe produced fluid in the oil/water separation process block and providea de-oiled water, wherein the de-oiling process block comprises an inletfor the produced water from the oil/water separation block and an outletfor the de-oiled water; a water treatment block operable to removecontaminants from the de-oiled water and provide a treated water,wherein the water treatment process block comprises an inlet for thede-oiled water and an outlet for the treated water; and a steamgeneration process block operable to produce steam from the treatedwater, wherein the steam generation process block comprises an inlet forthe treated water and an outlet for steam, wherein: each of theoil/water separation process block, the de-oiling process block, thewater treatment process block, and the steam generation process block ismodularized and comprises a plurality of modules; the de-oiling processblock comprises a compact flotation unit, the water treatment processblock comprises a mechanical vapor recompression evaporation apparatus,the steam generation process block does not comprise a once throughsteam generator (OTSG), or a combination thereof; the SAGD processingfacility comprises no pressure reduction apparatus, no temperaturereduction apparatus, or both no pressure reduction apparatus and notemperature reduction apparatus to reduce the pressure or thetemperature, respectively, of the produced water separated from theproduced fluid in the oil/water separation process block prior tointroduction of the separated produced water into the de-oiling processblock; or a combination thereof.

B: A method for operating a steam assisted gravity drainage processingfacility, the method comprising: effecting bulk separation of producedwater from a produced fluid comprising the produced water andhydrocarbons; removing residual oil from the produced water to provide ade-oiled water; removing contaminants from the de-oiled water to providea treated water; and generating steam from the treated water, wherein:each of the effecting bulk separation, the removing residual oil, theremoving contaminants, and the generating steam is performed via aplurality of modules; the removing residual oil from the produced wateris effected via compact flotation, the removing contaminants from thede-oiled water is effected via mechanical vapor recompressionevaporation, the generating steam from the treated water is not effectedvia a once through steam generator (OTSG), or a combination thereof; thetemperature, the pressure, or both the temperature and the pressure ofthe produced water separated from the produced fluid via the bulkseparation is not reduced prior to removing residual oil from theproduced water; or a combination thereof.

C: A method for assembling a steam assisted gravity drainage (SAGD)processing facility, the method comprising: providing a plurality ofmodules for each of a number of process blocks including: an oil/waterseparation process block (a) operable for bulk separation of producedwater from a produced fluid comprising the produced water andhydrocarbons, wherein the oil/water separation process block comprisesan inlet for the produced fluid and an outlet for the produced waterseparated from the produced fluid; a de-oiling process block (b)operable to remove residual oil from the produced water separated fromthe produced fluid in the oil/water separation process block and providea de-oiled water, wherein the de-oiling process block comprises an inletfor the produced water from the oil/water separation block and an outletfor de-oiled water; a water treatment block (c) operable to removecontaminants from the de-oiled water and provide a treated water,wherein the water treatment process block comprises an inlet for thede-oiled water and an outlet for the treated water; and a steamgeneration process block (d) operable to produce steam from the treatedwater, wherein the steam generation process block comprises an inlet forthe treated water and an outlet for steam, wherein each process block(a), (b), (c), and (d) includes an electrical and instrumentation (E&I)room on at least one of the plurality of modules for that process block;interconnecting the plurality of modules within process blocks (a), (b),(c), and (d); connecting process blocks (a) and (b), (b) and (c), and(c) and (d); and connecting each E&I room with a central control roomand a main electrical supply.

D: A steam assisted gravity drainage (SAGD) processing facilitycomprising: an oil/water separation process block operable for bulkseparation of produced water from a produced fluid comprising theproduced water and hydrocarbons, wherein the oil/water separationprocess block comprises an inlet for the produced fluid and an outletfor the produced water separated from the produced fluid; a de-oilingprocess block operable to remove residual oil from the produced waterremoved from the oil/water separation process block and provide ade-oiled water, wherein the de-oiling process block comprises a compactflotation unit comprising an inlet for the produced water from theoil/water separation block and an outlet for the de-oiled water; a watertreatment block operable to remove contaminants from the de-oiled waterand provide a treated water, wherein the water treatment process blockcomprises mechanical vapor recompression evaporation apparatuscomprising an inlet for the de-oiled water and an outlet for the treatedwater; and a steam generation process block operable to produce steamfrom the treated water, wherein the steam generation process blockcomprises a boiler comprising an inlet for the treated water and anoutlet for steam, wherein each of the oil/water separation processblock, the de-oiling process block, the water treatment process block,and the steam generation process block is modularized and comprises aplurality of modules.

Each of embodiments A, B, C, and D may have one or more of the followingadditional elements: Element 1: further comprising a disposal watertreatment process block operable to prepare a disposal water from thewater treatment process block for disposal. Element 2: wherein thedisposal water treatment process block consists primarily or solely ofsolids separation apparatus. Element 3: wherein a boiler of the steamgeneration process block provides at least 97% steam efficiency. Element4: wherein the boiler comprises a drum boiler or a circulation boiler.Element 5: wherein each of the oil/water separation process block, thede-oiling process block, the water treatment process block, and thesteam generation process block is modularized and comprises theplurality of modules, and further comprising a distributed electricaland instrumentation system, wherein each of the oil/water separationprocess block, the de-oiling process block, the water treatment processblock, and the steam generation process block comprises an electricaland instruments (E&I) room. Element 6: wherein the E&I room is locatedon at least one module of the plurality of modules. Element 7: furthercomprising a central control room, wherein each of the at least onemodules of the plurality of modules on which the E&I rooms are locatedis in communication with the central control room. Element 8: furthercomprising underground electrical distribution from a main electricalsupply to each of the at least one modules of the plurality of moduleson which the E&I rooms are located. Element 9: wherein each of theoil/water separation process block, the de-oiling process block, thewater treatment process block, and the steam generation process block ismodularized and comprises the plurality of modules, and wherein theplurality of modules comprise equipment modules and pipeway modules.Element 10: wherein a majority of the pipeway modules are located abovethe equipment modules. Element 11: wherein a majority of the equipmentmodules comprise a drain system below a floor level. Element 12: furthercomprising: a de-oiled water storage apparatus comprising an inletfluidly connected with the de-oiling process block, whereby de-oiledwater from the de-oiling process block can be introduced into thede-oiled water storage apparatus, and an outlet fluidly connected withthe water treatment process block, whereby stored de-oiled water can beintroduced into the water treatment process block; a boiler feed water(BFW) storage apparatus comprising an inlet fluidly connected with thede-oiling process block, whereby treated water from the water treatmentprocess block can be introduced into the BFW storage apparatus, and anoutlet fluidly connected with the steam generation process block,whereby stored, treated water can be introduced into the steamgeneration process block as BFW. Element 13: wherein the de-oiled waterstorage apparatus, the BFW storage apparatus, or both are pressurized.Element 14: wherein the SAGD processing facility comprises less thanabout 60 modules. Element 15: wherein each of the effecting bulkseparation, the removing residual oil, the removing contaminants, andthe generating steam is performed via a plurality of modules, andwherein each plurality of modules comprises an electrical andinstruments (E&I) room on at least one module thereof. Element 16:further comprising a central control room, wherein each of the at leastone modules on which the E&I rooms are located is in communication withthe central control room. Element 17: further comprising distributingelectricity, primarily below ground, from a main electrical supply toeach of the at least one modules on which the E&I rooms are located.Element 18: wherein: the de-oiling process block (b) comprises a compactflotation unit, the water treatment process block (c) comprises amechanical vapor recompression evaporation apparatus, the steamgeneration process block (d) does not comprise a once through steamgenerator (OTSG), or a combination thereof; the SAGD processing facilitycomprises no pressure reduction apparatus, no temperature reductionapparatus, or both no pressure reduction apparatus and no temperaturereduction apparatus to reduce the pressure or the temperature,respectively, of the produced water separated from the produced fluid inthe oil/water separation process block (a) prior to introduction of theseparated produced water into the de-oiling process block (b); or acombination thereof. Element 19: wherein connecting each E&I room withthe main electrical supply comprises underground connecting.

While several embodiments have been provided in the present disclosure,it should be understood that the disclosed systems and methods may beembodied in many other specific forms without departing from the spiritor scope of the present disclosure. The embodiments and present examplesare to be considered as illustrative and not restrictive, and theintention is not to be limited to the details given herein. Manyvariations and modifications of the invention disclosed herein arepossible and are within the scope of the invention. For example, thevarious elements or components may be combined or integrated in anothersystem or certain features may be omitted or not implemented. Also,techniques, systems, subsystems, and methods described and illustratedin the various embodiments as discrete or separate may be combined orintegrated with other systems, modules, techniques, or methods withoutdeparting from the scope of the present disclosure. Other items shown ordiscussed as directly coupled or communicating with each other may beindirectly coupled or communicating through some interface, device, orintermediate component, whether electrically, mechanically, orotherwise. Other examples of changes, substitutions, and alterations areascertainable by one skilled in the art and could be made withoutdeparting from the spirit and scope disclosed herein.

Numerous other modifications, equivalents, and alternatives, will becomeapparent to those skilled in the art once the above disclosure is fullyappreciated. It is intended that the following claims be interpreted toembrace all such modifications, equivalents, and alternatives whereapplicable. Accordingly, the scope of protection is not limited by thedescription set out above but is only limited by the claims whichfollow, that scope including all equivalents of the subject matter ofthe claims. Each and every claim is incorporated into the specificationas an embodiment of the present invention. Thus, the claims are afurther description and are an addition to the detailed description ofthe present invention. The disclosures of all patents, patentapplications, and publications cited herein are hereby incorporated byreference.

What is claimed is:
 1. A method for operating a steam assisted gravitydrainage processing facility, the method comprising: effecting bulkseparation of produced water from a produced fluid comprising theproduced water and hydrocarbons; removing residual oil from the producedwater to provide a de-oiled water; removing contaminants from thede-oiled water to provide a treated water; and generating steam from thetreated water, wherein a temperature, a pressure, or both thetemperature and the pressure of the produced water separated from theproduced fluid via the bulk separation is not reduced prior to theremoving residual oil from the produced water.
 2. The method of claim 1,wherein the temperature, the pressure, or both the temperature and thepressure of the produced water separated from the produced fluid via thebulk separation is not reduced during the removing residual oil from theproduced water.
 3. The method of claim 1, wherein each of the effectingbulk separation, the removing residual oil, the removing contaminants,and the generating steam is performed via a plurality of modules.
 4. Themethod of claim 3, wherein each plurality of modules comprises anelectrical and instruments (E&I) room on at least one module thereof. 5.The method of claim 4, wherein each of the plurality of modules furthercomprises a central control room, wherein each of the plurality ofmodules on which an E&I room is located is in communication with thecentral control room.
 6. The method of claim 4, further comprising:distributing electricity, not underground, from a main electrical supplyto each of the plurality of modules on which the E&I rooms are located.7. The method of claim 4, wherein each of the plurality of modulesfurther comprises an equipment module and a pipeway module.
 8. Themethod of claim 7, wherein the pipeway module is located above theequipment module.
 9. The method of claim 7, wherein the pipeway moduleof the plurality of modules is fluidly connected to at least one of aplurality of pipes in a common pipeway.
 10. The method of claim 4,wherein each of the plurality of modules further comprises a drainsystem below a floor level of the plurality of modules and notunderground.
 11. The method of claim 1, wherein removing residual oilfrom the produced water is effected via compact flotation.
 12. Themethod of claim 1, wherein removing contaminants from the de-oiled wateris effected via mechanical vapor recompression evaporation.
 13. Themethod of claim 1, wherein generating steam from the treated water isnot effected via a once through steam generator (OTSG).
 14. A method forassembling a steam assisted gravity drainage (SAGD) processing facility,the method comprising: providing a plurality of modules for each of anumber of process blocks including: an oil/water separation processblock (a) operable for bulk separation of produced water from a producedfluid comprising the produced water and hydrocarbons, wherein theoil/water separation process block comprises an inlet for the producedfluid and an outlet for the produced water separated from the producedfluid; a de-oiling process block (b) operable to remove residual oilfrom the produced water separated from the produced fluid in theoil/water separation process block by compact flotation and provide ade-oiled water, wherein the de-oiling process block comprises an inletfor the produced water from the oil/water separation process block andan outlet for de-oiled water; a water treatment process block (c)operable to remove contaminants from the de-oiled water and provide atreated water, wherein the water treatment process block (c) comprisesan inlet for the de-oiled water and an outlet for the treated water; anda steam generation process block (d) operable to produce steam from thetreated water, wherein the steam generation process block comprises aninlet for the treated water and an outlet for steam, wherein the SAGDprocessing facility comprises no pressure reduction apparatus, notemperature reduction apparatus, or both no pressure reduction apparatusand no temperature reduction apparatus to reduce the pressure or thetemperature, respectively, of the produced water separated from theproduced fluid in the oil/water separation process block (a) prior tointroduction of the separated produced water into the de-oiling processblock (b).
 15. The method of claim 14, wherein the SAGD processingfacility comprises no pressure reduction apparatus, no temperaturereduction apparatus, or both no pressure reduction apparatus and notemperature reduction apparatus to reduce the pressure or thetemperature, respectively, of the produced water within the de-oilingprocess block (b).
 16. The method of claim 14, wherein the de-oilingprocess block (b) comprises a compact flotation unit.
 17. The method ofclaim 14, wherein the water treatment process block (c) comprises amechanical vapor recompression evaporation apparatus.
 18. The method ofclaim 14, wherein the steam generation process block (d) does notcomprise a once through steam generator (OTSG).
 19. The method of claim14, wherein each process block (a), (b), (c), and (d) includes anelectrical and instrumentation (E&I) room on at least one of theplurality of modules for that process block; wherein the method furthercomprises: interconnecting the plurality of modules within processblocks (a), (b), (c), and (d); connecting process blocks (a) and (b),(b) and (c), and (c) and (d); and connecting each E&I room with acentral control room and a main electrical supply.
 20. The method ofclaim 19, wherein connecting each E&I room with the main electricalsupply comprises above ground connecting.